Process relating to gas purification by ammoniacal cuprous solutions



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mw 2% 119m J. GWDELY.

PROCESS RELATING T0 GAS PURIFICATION BY AMMONIACAL CUPROUS SOLUTIONS Filed August 16. 1923 WITNESS in other connections where Patented ug.. 24, lQZb.

NlED

JOSEPH G. DELY, 0H'

SYBACUSE, NEW YORK, ASSIGNOR T0 ATMOSPHERIC NITROGEN CORPORATION, OF SYRACUSE, NEW YORK, A. CORPORATION OF NEW YORK.

rnocnssnnra'rme rro Gas PURrrrca'rroN BY AMMONIAGAL CUriaoUs sorurr'ons.

Application med August 1e, 1923.' serial No. 657,682.

rlhis .invention relates in its more particular application to one part of the process of catalytically producing ammonia from nitrogen and hydrogen gas, to wit, that part of said process wherein gas intended for participation in the catalysis is to be purified with respect to the elimination of carbon monoxide therefrom. The invention contemplates a variety of advantageous objects and results which will appear in detail during the course ofthe specification.

The invention may be carried out in connection with apparatus such as is illustrated in the accompanying -drawings in which Fig. l represents diagrammatically the procedure as carried out in practice. Fig. Q-is a simplified diagrammatic representation of the same method of procedure and Fig. v3 is a possible modification.v

lt will be understood that in this-specication the invention will be described with lparticular reference to the process of malring synthetic ammonia, although it is apparent that the invention may be employed similar problems are encountered. Speaking generally, the synthetic ammonia process involves'the action of a catalyst upon gas containing nitrogen'andphydrogen in the proportion of1:3 and it will be apparent that for the purposes of such catalysis the gas should be as freeA as possible from impurities. According to that type of synthetic ammonia process which is known as the de Jahn process, the gases which are to participate in the catalysis are -rst produced as a'mixture in which the nitrogen content is approximately onethird of the sum of the hydrogen and carbon monoxide contents by volume. This gas is brought together with nsteam into contact with acatalyst adapted to the oxidation of vcarbon monoxide to carbon dioxide with the production of an equal volume ofhydrogen. The resulting gases are then sub]ect'edtoa pressure of approximately 95 atm. and while under such pressure treated for the removal of impurities. One of these impurities consists of a remnant of carbon monoxide'fwhich is eliminated by passing the gases under pressure through an ammoniacal cuprous solution. It is at this point that several problems and dilliculties havejarisen which it isv the object of the present invention to overcome.

In the drawings a represents the conduit through which the gases to be purified enter the tower l and b the conduit through which gases, deprived of their CO content, pass to the next operation. The tower 1 is filled with suitable packing material anda continuous supply of ammoniacal cuprous solution flows through it. The solution is for example an ammoniacal copper carbonate solution having the following composition .ex`

...pressed as grams per 100 cc. of solution:

total copper, 6-9; cupric copper, 0.3-0.5; ctallammonia, 11-16; total carbon dioxide,

Solutions of more or less copper content can be used, in which case a corresponding change in the other constituents can also be made.l However, the greater the cuprous copper content of the solution, the greater is its absorbing capacity vfor carbon monoxide. It is obvious that'th'e foregoing composition is given by way of illustration only,

and that the invention is applicable to any `ammoniacal cuprous solution which may bepperative for the purposes under considera- Referring again to the drawings, the pump 2 delivers a continuous supplyof the solution through the pipe c" into the tower 1,- such solution in its downward travel. ab-k sorbing the carbon monoxide from the `gas flowing upwardly through the tower 1 from a to @and the solution with the absorbed carbon monoxide leaving the tower through the pipe d. I prefer to earlyv out the fore# going treatment. at a low temperature instead of at ordinary or room tempera-ture and preferably at a temperaturenear the freezing point, but without causing the solut-ion to freeze or any of its dissolved components to 'separate out in solid forni. With a solution of the type hereinabove described and other conditions as described the preferred operating temperature is about zero degrees, at which temperature under. the

lstated-conditions substantially all of the this procedure will be elaborated at a later'k oint.

Referring again to the drawings and-pre supposing that the gas to be purified in the line a to b is under a pressure above atmospheric, reducing valve e serves the purpose of relieving the corresponding excess pressure of the circulating Huid. The Huid thus relieved of excess pressure enters the vessel 3 from which it continuously Hows into a tower 4. Any gas accompanying the Huid or becoming disassociated therefrom in the vessel 3 escapes through the pipe f and is led into the scrubbing tower 8. The liquid, after passing through the tower 4, Hows through g to a heat interchanger 5, thence through a steam preheater 6, and finally into the regenerator tank 7. The tower 4 may be of any desired construction and may, for example, be similar in that respect to tower 1, but as indicated in the drawing, smaller in size. A temperature of approximately 70 to 75 C. is preferably maintained in the regenerator tank 7 by the steam coil 9. From the regenerator tank 7, the hot liquid, now having a desired cupric copper concentration, Hows through the line z-e' in heat exchange relation with pipe g through the interchanger 5 and thence into the brine cooler 10. The temperature effect of these various arrangements is approximately as follows: The Huid enters the tower v4 at 15 to 20 C. and leaves the tower at approximately 30 C., the temperature being raised in the interchanger 5 and preheater 6 to approximately finally reaching 70'to 75 C.. in the regenerator'tank 7. By heating the solution to this temperature substantially all of the absorbed carbon monoxide is driven out and evolved from the solution. As the hot liquid from the regenerator tank 7 passes through the interchanger .5, its temperature is very materially reduced prior to its introduction into the brine cooler l0 in which the temperature of the liquid is brought to approximately zero. Air isV injected and brought into intimate contact with the solution in the regenerator tank 7 by means of the air lift 11, which withdraws a portion of the liquid from the pipe k, Whose part 12 is preferably of enlarged cross section and filled with suitable packing to assure intimatel'contact of the materials passing through.' The air thus introduced has the function of oxidizing cuprous y copper to the cupric condition and, by the proper control ofthe volumel of admitted air a relativelyconstant cupric condition may be'maintained at a point corresponding generally to a point inthe line i and said cuprio concentration at this point is, of

- .course, sulicient to assure preservation of at least some cu ric copper concentration in the solution by e time the circulating Huid again reaches the regenerator tank 7. -Any gas evolved in the regenerator tank 7 is caused-toiHow through Athe connection c into the tower4 and similar connections Z and mi may also be 'led to the tower 4 from the.

preheater 6 and the interchanger 5, respectively. Any'gas leaving the tower 4 Hows through the pipe fn, preferably joining the pipe f, the gas being led into the scrubbing tower, where it is scrubbed with water while the residual gas leaves through the outlet connection c. The effect of the operations is as follows: The solution recovered from the tower l contains substantially all of the CO which was present in the gas entering the tower l through a; The problem isto regenerate the solution economically to adapt it for re-use in a regenerated condition in the tower 1,', This is accomplished by the process thus far described. By the term regenerated I intehd to refer to a condition whereby the solution is restored to substantially the same condition in which .rit originally entered the tower 1, i. e., a condition such that the solution is substantially -freed from carbon monoxide and that an amount of-cuprous copper is oxidized to the cupric state equivalent to the amount of cuprlc copper which has been reduced to thel tion.' By this means the regenerated solution is returned to the solution inlet of tower 1 in a condition of relative constancy of composition. In the vessel 3 the gas which Hows out through f consists mainly of CO, nitrogen, and hydrogen. In the tower 4, therefore, the entering liquid contains practically all of the ammonia of the original solution. As the liquid is heated in the interchanger 5, the preheater 6 or the regenerator tank 7, there are driven off very substantial volumes of ammonia .and CO2 as well as CO. The function of the air-lift V11--12 is to maintain a certain amount lof cuprie .copper in the solution, afpart ofthe CO present in the solution being at the same time oxidized to CO2. Incidentally the air causes the tank 7 to give oif increased volumes of ammonia and CO2. Whatever ammonia or CO2 or CO are released or driven off during any part of the passage of the fluid through the tower 4 to the tower l, in-

cluding any gases added as the result of the lllli ratesof solubility of the various gases, and the condition ofthe liquid, a condition of selective absorption is maintained, such that the major portion of the ammonia gas is reabsorbed while only so much of the CO2 escapes as represents surplus CO.Z with respect to the proper constitution of the solution in its original state. ln' other words, only so much CO2 escapes through the towerl (except, ofcourse, such C02 as may be carried into the system at a) as is equivalent to the CO2 formed by the oxidation of CO through the air-lift 11 or otherwise it will be apparent that whatever taires place in the various parts of the system from the tower 4 onward, no gas is allowed to escape with-` out being first treated by the as yet unregenerated liquid inthe tower 4, and in the tower 4 the conditions are such as to be fa gas, the amount-of which is, however, insignificant when contrasted with the gas Ithat would have had to be added if the regeneration system had been conducted as an open system orA under conditions other than those described. This ammoniain the gas passing through n and f is recovered vas ammonia liquor in the scrubbing tower 8.

Obviously the temperature conditions prevailing in the tower 4 are of great importance and it should not'be so operated as to give a time of contact longer than is necessary for the desired ammonia retention. `When so'opera-ted it will be found that the absorption of the ammonia is selective with respect to the carbon dioxide of the gas. That is to say the carbon dioxide formed during the regeneration by .oxidation of some of the absorbed carbon monoxide (particularly in regenerator tank 7 and evolved, is not absorbed, but passes` out with the exit gas at n. Furthermore, as the solution in 4 is already relatively satuu rated with carbon monoxide, the absorption of the latter is small and in any case immaterial, as final regeneration takes place at points beyond the tower 4 in the apparatus 5, 6 and 7. The net result is that the major portion of the evolved ammonia and it only, is recovered and returned to the cuprous solution uncontaminated with injurious or objectionable impurities, such as carbon monoxide and carbon dioxide and that both the ammonia and CQ,V contents of the cuprous solution are maintained constant so that it can be used indefinitely; and all ofthis is accomplished without interference with or objectionable complication of the regenera tion procedure, but in direct conjunction therewith.

A certain amount of heatis evolved during the absorption in the tower 4 and it is advisable for efficient operation 'not to allow the temperature of the exit solutionto rise much above 30 C. and preferably not above 25 C. Practical experience with the process has demonstrated that over of been given,

@period without experiencing any the ammonia content of the gas evolved during the regeneration of a copper solution such as the one for which the formula has can be returned directly to the copper solution and with practically no re- I0 tention of the. carbon dioxide formed dur- 'ing regeneration so that the carbon dioxide content of the copper solution remains practically constant and unchanged.

By the terms pactically constant and unchanged l do not mean that the total carbon dioxide content of the copper lsolution remains continuously and absolutely tixed.. As a matter of fact, it does vary with changes in conditions suoli as the temperature of regeneration, temperature of operating the recovery tower 4, time of contact of gas in 4, etcy Then again, if the carbon dioxide content of the copper solution is initially relatively low with respect to its ammonia. content, it will at-first gradually increase in amountd until it reaches a valuecorresponding, for example, to that of 10 t0 15 grams per 100 ccuin the case of my pre ferred solution. The copper solution will then begin` to exert its full selective absorbing power in the tower 4 and no further permanent increase in its CO2 content will take place. Again, if the carbon dioxide content of the solution is initially high with respect to its ammonia content, it will at first gradually decrease in amount until it reaches a value corresponding to 10 to 15. grams per cc. in the case of my preferred solution and under the conditions of opera- 100 tion as described. In other words there is` no steady and continuous increase or decrease in the'tota'l carbon dioxide content of the cupper solution but a condition of equilibrium is soon reached, so that the same copper solution can he" used Ain conjunction with my recovery process for an indefinite diiiiculty due to its carbon dioxide content and without having to take any additional or special 11o measures for its control; for example, during a. months operation with a solution whose total copper content was 8 to9 grams per 100' cc. and the'total ammonia 14 to 17 y grams, the total CO2 content luctuated 115 within the range yof 10 to `l5 grams, and averaged 12.7 grams. For all practical opl erating` purposes, therefore, the totalcarbon dioxide content of the solution remains constant and it is in this sense that the solution is referredn t-o as remaining practically constant and unchanged. l l

This feature of the process holds true also in case the crude gas to be purified contains some CO, as well yas CO. In this case the C()2 ofthe gas evolved passing through f is equivalent to the C() oxidized to CO2 in the system plus the C()2 initially absorbed from the crude gas.

The ammonial content of the gas evolved during regeneration increases as the temperature ,of the regenerating solution 1s raised. The gas evolved from the regenerating apparatus 6 and 7 is therefore the most concentrated in ammonia and T have found that the advantages of my invention are obtained if in carrying out the process only the gas from 6 and 7 is passed through the recovery tower 4 while the gas from the interchanger 5, instead of leading through m into the tower 4, is allowed to communicate with the scrubbing tower 8 either directly or through connection with the lines n orA f. Generally, however, it is preferred to pass through the recovery tower 4 all of the gas evolved from the regenerator| solution after it leaves the recovery tower 4, i. e. all of the gas evolved either in 5, 6 or 7.

Attention has' already been called to the fact that the preferred temperature in the recovery tower 4 is not higher than between 15o to 25 C. This presupposes a temperature of approximately'zero of the solution entering the tower 1 through c. rl`he use of this temperature in the solution entering the tower 1 involves a number of incidental advantages of considerable importance. The capacity is increased without any loss in elficiency, i. e. the amount of-gas purified per unit of time with a given apparatus may ybe increased Without any unfavorable effect on degree of carbon monoxide removal; or the same amount of gas may now be purified to the same extent with a smaller apparatus. Furthermore, the carbon monoxide is more completely removed when the solution is maintained at the specified low temperature. This feature is of considerable importance in those cases in which the ammonia catalyst which ultimately operates upon the gases from b is or becomes increasingly sensitive to traces of carbon monoxide in the gas. Then again, less solution is required per unit of gas purified and when the low temperature solution is used, the water and carbon dioxide content' of the exit gas at o is decreased, a fact which simplifies and relieves the subsequent purification steps. The step of refrigerating the gases from b after treatment with the copper solution, which has heretofore been made use of in some instances, can be entirely eliminated. lt seems that the removal of carbon monoxide from a gas by means of a copper solution is due to a chemical reaction between thefrcarbon monoxide and copper with formation of a complex chemical compound containing both the copper and the carbon monoxide. lt was found by experiment that a low temperature copper solution, in spite of the fact that a decrease in temperature tends to decrease the rate. of a chemical reaction and therefore 4apparentlyV retards the formation of the complex copper compound, nevertheless causes an increase of net eHiciency probably due to memes the increased stability of the formed compound at the low temperature. Tt seems also to be the fact that after a certain degree of low temperature has been reached, no substantial increased efficiency will develop by reducing the temperature further.

specified conditions the cooling might be carried, say to *5 C., no appreciable advantage accrues therefrom over the use of a 0 C. temperature.

Attention is also called to the fact that the process described in this specification is av continuous process. Heretofore it has been proposed to regenerate the copper solution by a process which may be termed a batch process wherein the spent solution is collected in one storage tank for subsequent regeneration while the solution which circulates through the tower corresponding to 1 was withdrawn from a second tank containing regenerated solution, a third tank being simultaneously used for regeneration. When the second tank was empty,- it was used as the collecting tank for spent solution while the first tank was used for regeneration and the third tank, now containing-regenerated solution, was used to supply circulating liquid. That a continuous operation is far more satisfactory and more desirable in that less solution and less storage capacity is Thus, althoughwith the specified solution and the needed for a given installation, is apparent.

Operating conditions also are more uniform. It has been proposed to withdraw the spent solution from a tower corresponding to the tower 1 and at once to heat and blow air through the solution, returning it immediatcly to the tower. The solution under such conditions will not, however, remain constant in composition, so that, although the operation may be described as .continuous with reference to a short period of time, it cannot be fairly termed continuous when considered as an industrial process functioning day in and day out and without interruption month after month. Finally it is to be noted that the gas from o contains both all the carbon monoxide removed from the gas entering the system at a (with the exception of that small portion which was oxidized to carbon dioxide)and also all the nitrogen and hydrogen which as in the de Jahn process may be removed from the gas by solution in the copper fluid due to the excess pressure existing in tower 1. This gas, referring again to the de Jahn process, can now be returned to the crude nitrogenhydrogen-carbon monoxide gas before its treatment with steam and a catalyst. The result is that practically all the carbon monoxide of the crude gas is made available for the production of hydrogen and all this hydrogen and all the hydrogen and nitrogen of the crude gas is recovered and made available for ammonia synthesis.

the loss of ammonia `tion may result, in the case of the vpurificamenait question of tempera-ture control and some extra pipe lines. l

,2. A greatdecrease in ammonia consumed in the process. Without a recovery system yfrom the copper solution of a 3:1 hydrogen-nitrogen gas, to as much as 5% ofthe total ammonia produced view of the closed s :from the gas so purified.

3. The almost automatic the whole plant. Y

4. The maintenance of uniformoperating conditions .and consequently uniform 'results, the circumstance that every change in condition is a gradual 'one and that there are no sudden or violent variations or fluctuations of conditions at any point. rlLliis is a function of the continuous feature of my process. y

5. The certainty thatV no 'unregenerated solution will accidentally or otherwise be pumped through and get into tower 1. lin stem and the continuous nature of the de J a n ammonia process and the injurious edect of even so-called traces of CO on many ammonia catalysts, this feature'of my process is an important insurance, against poisoning of the catalyst and a guarantee of satisfactory operation of the ammonia process as a whole.

6. increased eiiiciency both as to economy vof operation and degree of purification as a functioning of result of the preferred low .temperature operationof my process.

7. The carbon monoxide, together with the nitrogen and hydrogen content of the evolved gas, if any, is recovered in such condition that it can -be returned to subsequent portions of the crude gas and thus utilized as originally intended. rllhere is no loss of the desirable ingredients vof the crude gas. This is of particular advantage in the application of my process to ammoniasynthesis.

rlhere are many other advantages but those which have been pointed out will suffice to show the importance in valuel of the invention. 'llt is, of course, understood that the invention is not limited to any particular process for the synthesis of ammonia, but can be l satisfactorily practiced in conjunction with any process which'involves the removal of or the production of carbon monoxide for any purpose and in which an ammoniacal cuprous solution is the removing agent. lt is also obvious that my invention is not limited to the particulartype or arrangement of ap aratus shown in Fig. 1 of the drawing. *or example, so far as the regeneration of the spent solution is concerned and the return of the evolved ammonia to the solution, the purposes of the apparatus 3, 4, 5, 6

and 7 may also be served by any suitable sequence of towers or even by a single tower through which the copper solution passes. Such an arrangement is illustrated in Fig. 3 in which. air is shown as being introduced at the bottom of the tower or tank 37 and the temperature throughout the tower is approximately regulated to correspond with the temperatures in 3, 4, 5, 6 and 7, respectively. rlhe liquid from the tower 1 is, in this case, passed directly through Z'to the regenerating and recovery tank or tower 37, and from the latter the liquid passes through h di rectly through d to the regenerating and recovery tankor tower 37, and from the latter the liquid passes through h directly to the brine cooler 10. At n and f the gases evolved pass out either to the absorber 8 or to some other use or to the stack. The operations as conducted in Fig. 3, although carried out in one (or more) towers are substantially like those of Fig. 1.

The regenerating processl may be conducted under reduced or increased pressure. In that case the temperature in tank 7 will obviously not have to be 7 0-75 C. but may be maintained respectively at a lower or higher temperature, and this is also true as to other temperatures in the regenerating system.

Should there be oxygen in the gases entering at a such oxygen as is absorbed by the copper solution will function in the re generating system to oxidize cuprous copper to cupric and some CO to C02, in approximately the same manner as the oxygen of the air introduced through the air lift 11. 'llhe 'fact that the regenerating system, considered from the standpoint of CO removal,` also has the capacity of dealing with absorbed oxygen'on lines directly in harmonyA with CO removal, rous absorption process with the described regenerating system of special advantage for the purification of ammonia synthesis gas, since that gas requires almost. complete freedom from oxygen before it can be submitted to the catalyst.

l claim:

1. That improvement in the processor" recovering ammonia from gas evolved in the regeneration of ammoniacal cuprous solution containing carbon monoxide which comprises treating the elolved gas with unreenerated ammoniacal cuprous solution.

2. That improvement in the process'of recovering ammonia from gas evolved in the regeneration of ammoniacal cuprous solution containing carbon monoxide which comprises treating the evolved gas with unregenerated ammoniacal cuprous solution and then with a liquid capable of absorbing aminonia.

3. In the process of removing carbon mon oxide from gas mixtures b. treating the mixture with an ammoniaca cuprous solution that improvement Which comprisesl bringing the gas evolved in the regeneration of the copper solution into Contact with unregenerated ammoniacal cuprous solutlon.

4. In the process of removing carbon monoxide from gas mixtures containing it by means ot ammonlacal cuprous solution thatv unprovement which comprises bringing the gas evolved at a stage of the regeneration 6. ln the art of removing carbon monox-v ide from gas mixtures by means ot ammoniacal cuprous solution and of restoring the efficiency ot such cuprous solution that improvement which comprises gradually raising its temperature in stages and bringing the gas evolved at one temperature stage into contact with solution at an earlier stage.

7. rllhat improvement in the process ot removing carbon monoxide from gas mixtures which comprises circulating ammoniacal cuprous solution in contact With and countercurrent tothe gas mixture, then circulating the resultant spent solution through '-zones ot gradually increasing temperature,

While circulating further portions of the spent solution in Contact with the evolved gas thereby causing .liberation of the absorbed carbon monoxide and reabsorption ot ammonia evolved at the higher temperatures and linally recirculating that part of the solution which has passed through the region of highest temperature in contact with and countercurrent to further quantities of the gas mixture.

S. The process of depriving a gas mixture of its carbon monoxide content by bringing the gas mixture into contact with` ammoniacal cuprous solution at a pressure above atmospheric, releasing the pressure of the spent solution to about atmospheric, gradually heating the solution to cause yremoval therefrom vof carbon monoxideybringlng portions ot the spent solution into contact With -the gas from the heated solution, passing an oxygen-bearing gas through that portion ot the solution which has been subjected to the maximum temperature treatment and then cooling and bringing the cold regenerated solution into contact With further quantities of the gas to be puriied, thus completing the cycle.

solution, regenerating the resulting spent ammoniacal cuprous solution by gradually raising its temperature and treating 1t With v oxygen containing gas, bringing the thus reenerated cuprous solution into contact with urther quantities of the carbon monoxide containing gas thus completing the cycle and recovering ammonia from gas evolved during regeneration of the copper solution and returning it to the cuprous solution by bringing the evolved gas into contact with unregenerated solution. l0. That improvement in the process of utilizing the carbon monoxide of a gas mixture inthe manufacture of hydrogen7 suitable for ammonia synthesis, Which consists in bringing the gas in the presenceot steam into contact with a catalyzer suitable for the oxidation ,of carbon monoxide to carbon dioxide with the production of an equal volume of hydrogen, absorbing the residual unconverted carbon monoxide in ammoniacal cuprous solution,;recovering the absorbed carbon monoxide by circulating such cu- `Vprous solution through zones of gradually increasing temperature to cause evolution of creasing temperature to cause evolution of the said carbon monoxide from the said solution; and Iinally returning the recovered carbon monoxide to the ravv gas supply for renewed exposure to the catalyst.

ll. That improvement in the process of preparing a gas mixture containing nitrogenand hydrogen in the proportion of one.

to three which comprises producing a gas mixture in which the nitrogen content is approximately one-third of the sum of the hydrogen and carbon monoxide content by volume, bringing the gas together With steam L into contact With a catalyst adapted to the oxidation of carbon monoxide to carbon dioxide With the production of an equal volume of hyogen, absorbing the residual unconverted carbon monoxide in ammoniacial cuprous solution, recovering the absorbed carbon monoxide together with dissolved nitrogen and hydrogen by heating such cul prous solution gradually and bringing the 'gas evolved at the higher temperatures into contitl tact with ammoniacal cuprous solution at the lower temperatures and finally' returning the resultant recovered gas to the gas mixture prior to its exposure to the catalyst.

l2. The process which consists in bringing a gaseous mixture containing carbon monoxide, in contact with an ammoniacal cuprous solution which Will remove such carbon monoxide from said gaseous mixture, separating the purified gas from the solution,-

bringing the solution'to a higher temperature to drive out the absorbed carbonmonoxide, treating the solution with an oxygenbearing gas; refrigerating the solution after removal ot' the carbon monoxide and after the said oxidation treatment, and returning the cooled regenerated solution to renewed contact with gases to be deprived of their carbon monoxide content.

13. The process which consists in bringing a gaseous mixture containing carbon monoxide, in contact with an ammoniacal cuprous solution which will remove such carbon monoxide from said gaseous mixture, separating the purified gas from the solution,

monoxide, in Contact with an ammoniacal cuprous solution which'will remove such carbon monoxide from said gaseous mixture, separating the puritied gas from the solution, bringing the solution to a higher temperature by successive steps, driving out ammonia and absorbed carbon monoxide, conducting such ammonia from a step of higher temperatureback into contact with the solution at a point of lower temperature land at the highest temperature injecting air to complete the regeneration of the solution; removing from the system at a lower temperature point carbon dioxide together with the carbon monoxide. and any other constituents there remaining in 'gaseous form, retrigerating the regenerated solution and returning the cooled regenerated solution to renewed contact with gases to loe deprived ot their carbon monoxide content.

15. The process which consists in bringing.

a gaseous mixture containing carbon monoxide, in contact with an ammoniacal cuprous solution which will remove such carbon monoxide from said gaseous mixture, separating the purilied gas from the solution, bringing the solution to a higher temperature by successive steps driving out am- -monia and absorbed carbon monoxide, conducting such ammonia 'from a step of highery temperature back into contact with the solution at a point of lower temperature, re-

generating the solution from which the gases were evolved, refrigerating the regenerated solution, strengthening the regenerated ainlnoniacal cuprous solution with ammonia 'from an outside source, and returning the cool regenerated solution to renewed contact with gases to be deprived of their carbon monoxide content.

16. The process which consists in bringing a gaseous mixture containing carbon monoxide, in contact with an ammoniacal cuprous solution which will remove such carbon monoxide rom said gaseous mixture, separating the puritied gas from the solution, bringing the solution to a higher temperature by successive steps, driving out ammonia and absorbed carbon monoxide, conducting such ammonia from a step of higher temperature back into contact with the solution at a point of lower temperature and at the highest temperature injecting air to complete the regeneration of the solution; removing from the system at a lower temperature point carbon dioxide together with the carbon monoxide and any other constituents there remaining in gaseous form, refrigerating the regenerated solution, strengthening the regenerated ammoniacal cuprous solution with ammonia from an outside source and returning the cool regenerated solution to renewed contact with gases to be ideprived of their carbon monoxide content.

17. The process of freeing gases from carbon monoxide which consists in continuously subjecting such gases to an ammoniacal cuprous solution capable of absorbingcarbon monoxide, continuously flowing the solution from said absorption stage through a regenerating system and the regenerated solution bacia tothe absorption stage, continuously withdrawing the gases evolved in the regenerating system and at a predetermined part of said regenerating system establishing and maintaining a condition ot predetermined constancy of composition of the solution.

18. That improvement in the process of recovering ammonia from gas evolved in the regeneration of ammoniacal cuprous solution containing carbon monoxide, which comprises treating the evolved gas with unregenerated ammonlaeal cuprous solution while treating that-portion of the solution from which the gas was evolved, with an oxygen-bearing' gas.

In testimony whereof I have hereunto set my hand.

JOSEPH DELY.

, Certicate ot Correction.. n It is hereby certified that in Letters Patent No. 1,5197 ,345, granted August 24, 1926,

upon the application ment in Processes of Joseph G. Dely, of S -*racuse, Relating to Gras Purification byl Ammoniacal Cuprous VSolu- New York, for an improvetions, errors appear in the printed specification lrequiring correction as follows:

Page 2, line 70, for the letter read eval/ved; and that the said Letters c read o; page 3, line 3,- for read other/wise. It will; page 5, line 11S, claim 1,

otherwise it will for the misspelled word elolved Patent should be read with these corrections therein that the same may conform to the record of the case in the Patent Office.

Signed and sealed this 2d day of November, A. 1926.

[smul vWM. A. KINNAN, Acting Commissioner of Patents. 

